System and method for production of on-demand proteins in a portable unit for point of care delivery

ABSTRACT

A portable and mobile bioprocessing system and method for protein manufacturing that is compact, integrated and suited for on-demand production of any type of proteins and for delivery of the produced proteins to patients or for assay purposes. The portable system and method can also be used for efficient on-demand production of any type of protein with point-of-care delivery.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a divisional of co-pending U.S. patent applicationSer. No. 16/506,079 filed on Jul. 9, 2019, which is a divisional of U.S.patent application Ser. No. 15/966,609 filed on Apr. 30, 2018, now U.S.Pat. No. 10,435,664, which is a continuation of U.S. patent applicationSer. No. 15/095,305 filed on Apr. 11, 2016, now U.S. Pat. No. 9,982,227,which is a continuation-in-part application of U.S. patent applicationSer. No. 13/823,911, filed on Jun. 28, 2013, now U.S. Pat. No.9,388,373, which in turn was a 371 application of PCT Application No.PCT/US2012/028358, filed on Mar. 8, 2012, which in turn claims priorityto U.S. Provisional Application Ser. No. 61/450,191, filed Mar. 8, 2011,the contents of all is hereby incorporated by reference herein for allpurposes.

GOVERNMENT RIGHTS IN INVENTION

This invention was made with government support under Grant NumberN66001-13-C-4023 awarded by the Defense Advanced Research ProjectsAgency (DARPA). The government has certain rights in the invention.

BACKGROUND OF THE INVENTION Field of the Invention

The present invention relates to protein manufacturing and, moreparticularly, to an integrated and compact bioprocessing system foron-demand production or manufacturing of proteins for point-of-caredelivery.

Background of the Related Art

The time it takes for a new drug to reach the market is 8-10 years at acost approaching $1.2 billion. Many of these new drug entities arereferred to as biologics (e.g., a protein used as a drug ortherapeutic). These are molecules produced by living cells in vitrousing cell culture and fermentation technologies. Stringent processcontrol is required since changes in culture conditions can lead to, forexample, altered glycosylation profiles, which can then drasticallychange the drug's pharmacokinetics, efficacy and immunogenicity.Therefore, much effort towards FDA approval is devoted to thedevelopment of documented and robust manufacturing processes that willproduce safe and efficacious biologics of consistent quality. These arecollectively referred to as good manufacturing processes (GMP). The goalis to arrive at a process that is well defined and reproducible, andthat leads to products that meet pre-determined characteristics ofquality, identity, purity, safety and efficacy.

Biologics are currently produced in a centralized manufacturing facilitywith large scale (>10,000 liters) cell cultures, and with the necessarylarge volume separation, purification, formulation, packaging, anddistribution infrastructure (e.g. a typical Merck, Pfizer or Genentechplant). The time period from a cell bank to the final delivery of thetherapeutic vial is on the order of 6-8 weeks under ideal conditions andproduces batches of around 10 Kg bulk protein. As shown in FIG. 1, theprocess itself is complex. FIG. 1 shows a typical flow sheet for themanufacturing of protein biologics--both for proteins that are expressedintracellularly and proteins expressed extracellularly. Every step needsto be individually developed, scaled-up, optimized and validated in amanufacturing setting. The final product will also have an expirationdate and is either shipped lyophilized or via a cold chain, which mustalso be documented.

Thus, there is a need for production of biological medicines inreal-time and/or on-demand to provide therapeutic proteins in remotelocations. Also, there is a need for a system and method of preparingtherapeutic proteins with increased activity with the possibility ofreduced amount of preservation, enhancing and/or stabilizing excipientsbecause of the immediate and/or timely use of such therapeutic proteins.

A similar opportunity exists for proteins in non-therapeuticapplications. By their nature, proteins are unstable and requirepreservation by a variety of methods to preserve their activity. Theyare widely used in the diagnostics industry, in food and cosmetics. Inthese cases as well, the ability to manufacture fresh protein on-demandwould be of great benefit.

SUMMARY OF THE INVENTION

The present invention provides for an integrated and compactbioprocessing system and method for the production of proteins withincreased activity with the possibility of reduced amount ofpreservation, enhancing and/or stabilizing excipients because of theimmediate and/or timely use of therapeutic proteins and diagnosticproteins, where a critical assay is to be performed.

In one aspect, the present invention provides a portable and compactbioprocessing system for the production of proteins for point-of-caredelivery.

In another aspect, the present invention provides for an integrated andcompact bioprocessing system for protein expression and purification.

In yet another aspect, the present invention provides for a method foron-demand production and delivery of a therapeutic protein to a patient.

In a still further aspect, the present invention provides for a portablesystem and method for on-demand production of a therapeutic proteinprepared in a composition with reduced amounts of stabilizers,oxidation/reduction agents and/or other excipients.

In another aspect, the present invention provides for a portable systemand method for on-demand production of a therapeutic protein, whereinthe therapeutic protein exhibits increased potency due to the timelysynthesis and substantially immediate delivery of protein. Preferably,the newly synthesized proteins are delivered to a patient within onehour, to one day, to two weeks. Preferably any refrigeration is at atemperature above freezing from 0 to 6° C. Any freezing of the proteinsis preferably a single event with temperatures ranging from about −2° C.to about −10° C.

In yet another aspect, the present invention provides for a portablesystem and method for on-demand production of a therapeutic protein,wherein the produced therapeutic protein can be delivered continuouslyor as a bolus as it is produced and as it happens physiologically, wherethe body produces needed proteins over an extended time in vivo and whenneeded.

A still further aspect, the present invention provides for a freshlysynthesized protein in a composition, wherein the freshly synthesizedprotein is synthesized on-demand and exhibits increased activity, andwherein a buffering composition comprising the freshly synthesizedprotein is essentially lacking a stabilizer.

To achieve at least the above aspects, in whole or in part, there isprovided a bioprocessing system comprising a production module forproducing a protein and a purification module for receiving the proteinfrom the production module and for purifying the protein from reagents.The bioprocessing system may further comprise a processor forcontrolling and/or monitoring at least the production module and/or thepurification module. The processor is communicatively connected to atleast the production module and/or purification module to control thetiming, temperature and other parameters necessary for optimizing theproduction and purification of the synthesized proteins to provide asufficient amount of or a therapeutic dosage of the synthesized protein.Such length of time in the production module and/or purification modulemay be used to affect the potency and/or activity of the synthesizedprotein.

To achieve at least the above aspects, in whole or in part, there isalso provided a bioprocessing system, comprising a reactor for proteinexpression, a membrane chromatography component for receiving andpurifying protein output by the reactor and a diafiltration componentfor receiving purified protein from the membrane chromatography and forfurther purifying the purified protein.

Additional advantages, aspects, and features of the invention will beset forth in part in the description which follows and in part willbecome apparent to those having ordinary skill in the art uponexamination of the following or may be learned from practice of theinvention. The aspects and advantages of the invention may be realizedand attained as particularly pointed out in the appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

The invention will be described in detail with reference to thefollowing drawings in which like reference numerals refer to likeelements wherein:

FIG. 1 shows a typical flow sheet for the manufacturing of proteinbiologics, both for proteins that are expressed intracellularly andproteins expressed extracellularly.

FIG. 2 is a block diagram that illustrates the principles of operationof one preferred embodiment of the present invention.

FIG. 3 is a schematic diagram of a bioprocessing system, in accordancewith another preferred embodiment of the present invention.

FIG. 4 is a schematic diagram of a microscale bioprocessing system, inaccordance with another embodiment of the present invention.

FIG. 5 is a side schematic view of a membrane chromatography componentthat can be used in the systems of FIGS. 3 and 4, in accordance with thepresent invention.

FIG. 6A is a top plan view of a microfluidic diafiltration componentthat can be used in the systems of FIGS. 3 and 4, in accordance with thepresent invention.

FIG. 6B is a schematic cross-sectional view of the equilibrium chamberof FIG. 6A looking along the cross-section line A-A of FIG. 6A.

FIG. 6C is a bottom plan view of the equilibrium chamber of FIG. 6A.

FIG. 7 is a perspective schematic view of another microfluidicdiafiltration component that can be used in systems of FIGS. 3 and 4, inaccordance with the present invention.

FIG. 8 is a diagram showing the main steps in in vivo proteinexpression.

FIG. 9A shows results for the expression of G-CSF from different runs(Run #3) and showing the reproducibility.

FIG. 9B shows results for the expression of G-CSF from different runs(Run #4) and showing the reproducibility.

FIG. 10A shows the quantified values for Run#3 of FIG. 9A.

FIG. 10B shows the quantified values for Run#4 of FIG. 9B.

FIG. 11 shows the potency results of recombinant human G-CSF from Run #3and Run #4.

FIG. 12 shows the Western blot of quadruplicate run of EPO in dialysiscassettes prior to purification.

FIG. 13 A shows EPO expression in stirred tank bioreactor and FIG. 13 Bshows Streptokinase expression in stirred tank bioreactor.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

The present invention is particularly suited for the on-demandmanufacturing of therapeutic proteins (either cell-based or cell-free)that are suitable for direct delivery to a patient. Therefore, thepresent invention will be primarily described and illustrated inconnection with the manufacturing of therapeutic proteins. However, thepresent invention can also be used to manufacture any type of protein,including toxic proteins, proteins with radiolabeled amino acids,unnatural amino acids, etc. Further, the present invention isparticularly suited for the on-demand manufacturing of proteins usingcell-free expression, and thus the present invention will be describedprimarily in the context of cell-free protein expression. However, thepresent invention can also be used in connection with cell-based proteinexpression.

FIG. 2 is a block diagram that illustrates the principles of operationof one preferred embodiment of the present invention. The bioprocessingsystem 100 includes a production module 200, a purification module 300and a fluid storage/dispensing module 400 that are fluidly coupled viacoupling components 500. A processor 600 may be in electricalcommunication with one or more of the production module 200,purification module 300, coupling components 500 and fluidstorage/dispensing module 400 for controlling and monitoring theoperation of the system 100.

The fluid storage/dispensing module 400 is adapted to store thesolutions needed for the production of a protein. The fluidstorage/dispensing module 400 may also include containers for storingany waste product produced during the production of the protein. Thefluid storage/dispensing module 400 may be temperature controlled, ifneeded, to maintain the solutions at a required temperature.

The production module 200 is adapted to receive the solutions requiredfor production of a protein, such as a therapeutic protein, from thefluid storage/dispensing chamber via coupling components 500. Theproduction module 200 may suitably include a bioreactor adapted formaintaining living cells that incorporates non-invasive optical chemicalsensing technology for monitoring culture parameters (e.g., pH, oxygen,optical density, fluorescence, absorbance, redox, temperature, etc.),such as the bioreactors and optical chemical sensing technologyillustrated and described in commonly assigned and related U.S. Pat.Nos. 6,673,532 and 7,041,493, as well as co-pending commonly assignedand related U.S. patent application Ser. No. 12/991,947, whosedisclosures are incorporated by reference herein in their entirety.These types of bioreactors are particularly suited for cell-basedproduction of therapeutic proteins. Alternatively, the production module200 may suitably include a stirred mini-reactor such as, for example,the BioGenie Minibioreactor sold by Scientific Bioprocessing, Inc., thatis adapted for the cell-free production of a protein, and that are alsoequipped with sensors for monitoring reaction parameters (e.g., pH,oxygen, optical density, fluorescence, absorbance, redox, temperature,etc.).

The production module 200 as illustrated in FIG. 2 is designed for batchmode protein production where all the components for protein production(DNA, cell-free lysate, reaction buffer, etc.) are combined in a singlestep and then delivered to the purification module via couplingcomponents 500 at the end of the reaction (3-6 hours). The productionmodule 200 may also be a cup with a dialysis membrane bottom or adialysis cassette with dialysis membrane on both sides. The cup orcassette will be surrounded by a dialysis buffer to remove reactionwaste products such as inorganic phosphate, but also to maintain theconcentration of nutrients such as amino acids and creatine phosphate.The solutions for protein production are delivered to the dialysis cupor the dialysis cassette and the surrounding dialysis buffer from thefluid storage/dispensing chamber 400 via coupling components 500.

After the reaction is complete, the raw product is then transferred tothe purification module 300 via coupling components 500. Thepurification module 300 contains the necessary purification componentsfor purifying the protein from the reagents. The purification module 300can include, for example, chromatography components and dialysescomponents for purifying the biologic.

The production module 200 and the purification module 300 may eachinclude sensors for monitoring reaction parameters and/or productquality parameters. The parameters monitored can include, but are notlimited to, conductivity, temperature, pH, oxygen and CO₂. The sensorsmay be any type of invasive sensor known in the art for monitoring theseparameters, where the sensors are in contact with the process fluid. Inaddition, the sensors may be non-invasive optical chemical sensors, suchas those described in U.S. Pat. Nos. 6,673,532 and 7,041,493, and U.S.patent application Ser. No. 12/991,947. In addition, spectrometers knownin the art can be used in the production module 200 and/or thepurification module 300 to monitor the product stream and/or the inputsto each module. The parameters measured by such spectrometers caninclude, but are not limited to, absorbance, fluorescence, Ramanscattering, circular dichroism and infrared spectral characteristics.

FIG. 3 is a schematic diagram of a bioprocessing system 700, inaccordance with another preferred embodiment of the present invention.The system 700 is particularly suited for the cell-free production ofproteins and will be described in this context.

The system 700 includes a reactor 210, in which protein expression takesplace, a membrane chromatography component 310, a diafiltrationcomponent 320 and a fluid storage/dispensing module 400. The reactor 210preferably includes a heating and cooling element 220, suitably athermoelectric cooler, for controlling the temperature of the solution230 inside the reactor 210. The reactor also preferably includes sensors240 and 250 for monitoring parameters in the reactor solution 230, suchas pH, oxygen, redox, conductivity or any other parameter that can bemeasured with existing sensors. The sensors 240 and 250 can beimplemented with any type of sensor known in the art for measuring thedesired parameters. However, the sensors 240 and 250 are preferablynon-invasive optical chemical sensors.

The system 700 also includes a processor 600 that is in communicationwith one or more of the reactor 210, optoelectronics 270, membranechromatography component 310, diafiltration component 320, fluidstorage/dispensing module 400 and pumps 520A and 520B for controllingand/or monitoring the operation of the system 700.

Optoelectronics 270 are provided for exciting the optical chemicalsensors 240 and 250 with excitation light 242 and 244, respectively, andfor receiving and detecting emission light 246 and 248 from the opticalchemical sensors 240 and 250, respectively. As discussed above, commonlyassigned and related U.S. Pat. Nos. 6,673,532 and 7,041,493, as well asco-pending commonly assigned and related U.S. patent application Ser.No. 12/991,947 describe in more detail how non-invasive optical chemicalsensing technology can be used to monitor parameters.

In FIG. 3, two optical chemical sensors 240 and 250 are shown, and arepreferably adapted to measure pH and dissolved oxygen, respectively.However any number of optical chemical sensors (including only one) maybe used depending on the number and type of parameters being measured.Optoelectronics 270 include optical excitation sources (not shown) forgenerating the excitation light 242 and 244, as well as photodetectors(not shown) for detecting the emission light 246 and 248 from theoptical chemical sensors 240 and 250. The type of optical excitationsource or sources are the types used in optoelectronics. Any combinationof optical excitation sources and optical chemical sensors may be used,depending on the number and types of parameters being measured. Examplesof optical excitation sources that can be used included inoptoelectronics 270 include, but are not limited to, light emittingdiodes and laser diodes. Alternatively, the optoelectronics 270 may justbe used to measure optical properties of the reactor contents in theirentirety absent any sensors.

Further, for each optical chemical sensor 240 and 250, two possibleplacements on the reactor 210 are shown. The two possible placements foroptical chemical sensor 240 are shown as 240A and 240B. The two possibleplacements for optical chemical sensor 250 are shown as 250A and 250B.The use of other non-contact sensors (i.e. Raman, contact freeconductivity sensors etc) is also possible in this context.

In the “A” placement (240A and 250A), the optical chemical sensors 240Aand 250A are positioned inside the reactor 210 on a reactor wall 260.With this placement, the optical chemical sensors 240A and 250A are inphysical contact with the solution 230, and the reactor wall 260 onwhich the optical chemical sensors 240A and 250A are placed is opticallytransparent to the excitation light 242 and 244, so that the excitationlight can reach the optical chemical sensors 240A and 250A.

In the “B” placement (240B and 250B), the optical chemical sensors 240Band 250B are positioned outside the reactor 210 on reactor wall 260.With this placement, the thickness of the reactor wall 260 issufficiently small so as to allow the analytes that are being measuredto diffuse through the reactor wall 260 and contact the optical chemicalsensors 240B and 250B. Alternatively, the portions of the reactor wall260 on which the optical chemical sensors 240B and 250B are attached canbe replaced with barrier membranes 249A and 249B that are adapted toallow the analytes being measured to diffuse through so that they comein contact with optical chemical sensors 240B and 250B. The use ofbarrier membranes and thin reactor walls to effectuate diffusion of theanalytes of interest through a container wall to optical chemicalsensors is described in more detail in commonly assigned and relatedU.S. patent application Ser. No. 13/378,033, which is incorporatedherein by reference in its entirety.

In the FIG. 3 embodiment, the fluid storage/dispensing module 400preferably includes a buffer solution container 410 for holding buffersolution, an mRNA/DNA solution container 420 for holding mRNA/DNAsolution, a reaction solution container 430 for holding reactionsolution, a waste storage container 440 for holding waste solution and aproduct storage container 450 for holding the purified protein. Inoperation, reaction solution, mRNA/DNA solution and buffer solution aredirected to reactor 210 via conduits 510A, 510B, 510C and pump 520A.

After the reaction in the reactor 210, the raw product is directed tomembrane chromatography component 310 via conduit 510E and pump 520B forpurification of the protein from the reagents. Membrane chromatographycomponent 310 may suitably include a cylindrically shaped housing whichcontains porous membrane layers (preferably at least 10 porous membranelayers), where the individual membranes consist of an appropriatepolymer, such as polymethacrylate, that has been chemicallyfunctionalized with a ligand, such as a diethylaminoethyl (DEAE), aquaternary amine (Q), or a carboxymethyl (CM) ligand for the case ofion-exchange chromatography, or a phenyl or butyl ligand for the case ofhydrophobic interaction chromatography, or a mercaptoethylpyridine (MEP)ligand for the case of mixed mode chromatography. One preferredembodiment of the membrane chromatography component 310 will bediscussed in more detail below in connection with FIG. 5. Waste from themembrane chromatography process is directed to waste storage container440 via conduit 510F. The purified product is directed to diafiltrationcomponent 320 for dialysis via conduit 510G and pump 520C.

Membrane chromatography component 310 may also include one or moresensors 312 for monitoring product quality parameters, such asconductivity, temperature, pH, oxygen, CO₂, absorbance, fluorescence,Raman, circular dichroism and infrared spectral characteristics. Thesensors 312 may be any type of invasive or noninvasive sensor known inthe art for measuring these parameters including, but not limited to,spectrometers. In addition, the sensors may be non-invasive opticalchemical sensors, such as those described in U.S. Pat. Nos. 6,673,532and 7,041,493, and U.S. patent application Ser. No. 12/991,947. Inaddition, membrane chromatography component 310 preferably includes aheating and cooling element 314, suitably a thermoelectric cooler, forcontrolling the temperature of the solution (raw product) inside themembrane chromatography component 310.

The diafiltration component 320 may suitably include a hydrophilicpolymeric membrane for use as a separation mode for dialysis forseparating proteins in a diluent liquid on the basis of differences intheir ability to pass through a membrane or in the alternative fordiafiltration to simply exchange the buffer solutions. Such hydrophilicpolymeric membrane may include, but not limited to, polyethersulfone, acellulosic, or a polyvinylidene fluoride (PVDF) membrane with awell-defined pore structure that yields a desired molecular weightcut-off (MWCO) value in the range of 10 k to 200 k Da as appropriate fora given application. The final protein that comes out of thediafiltration component 320 is directed to product storage container 450via conduit 510H. The waste product produced from the dialysis processin the diafiltration component 320 is directed to waste storagecontainer 440 via conduit 510I.

Diafiltration component 320 may also include one or more sensors 322 formonitoring product quality parameters, such as conductivity,temperature, pH, oxygen, CO₂, absorbance, fluorescence, Raman, circulardichroism and infrared spectral characteristics. The sensors 322 may beany type of invasive or noninvasive sensor known in the art formeasuring these parameters including, but not limited to, spectrometers.In addition, the sensors may be non-invasive optical chemical sensors,such as those described in U.S. Pat. Nos. 6,673,532 and 7,041,493, andU.S. patent application Ser. No. 12/991,947.

In addition, diafiltration component 320 preferably includes a heatingand cooling element 316, suitably a thermoelectric cooler, forcontrolling the temperature of the solution (raw product) inside themembrane chromatography component 320.

In addition to the pumps 520A, 520B and 520C, any number of valves orother hydraulic components, such as additional pumps, may be usedthroughout the system 700 to assist in controlling the flow ofsolution/product between the various components of the system 700.

The present invention is particularly suited to miniaturization by usingmicropumps and microfluidic technology. FIG. 4 is a schematic diagram ofa microscale bioprocessing system 800, in accordance with anotherembodiment of the present invention. The system 800 includes many of thesame components of the system 700 of FIG. 3, and common elements arelabeled with common element numbers.

The system 800 contains a fluid storage/dispensing module 400 thatincludes a buffer solution container 410 for holding buffer solution, anmRNA/DNA solution container 420 for holding mRNA/DNA solution, areaction solution container 430 for holding reaction solution, a wastestorage container 440 for holding waste solution and a product storagecontainer 450 for holding the purified protein. The system 800 alsoincludes a reactor 210, a membrane chromatography component 310, adiafiltration component 820, a processor 600, optical chemical sensors840 chosen and positioned to monitor finished product qualityparameters, such as, for example, conductivity, redox, pH, UV spectrumand protein concentration, and optoelectronics 830 for providing opticalexcitation light and for detecting emission light from the opticalchemical sensors 840. The optoelectronics 830 may also just be used tomeasure the optical properties of the finished product absent anysensors.

The reactor 210 can be of any size, but in the microscale embodiment ofFIG. 4, it preferably has a volume capacity of less than approximately50 milliliters, and more preferably approximately 20 milliliters orless, in order to keep the system 800 relatively compact. The reactor210 may be implemented, for example, with the BioGenie minibioreactorsystem manufactured by Scientific Bioprocessing, Inc.

Micropumps 850A and 850B and conduits 510A-510I direct solution to thevarious components in a manner similar to pumps 520A, 520B and conduits510A-510I in the system 700 of FIG. 3. Although not shown in FIG. 4, thereactor 210 contains optical chemical sensors and optoelectronics formonitoring parameters in the reactor solution 230 in a manner similar tosystem 700 of FIG. 3. The micropumps 850A and 850B may be implementedwith any type of micropump known in the art such as, for example, themp5 micropump or the mp6 micropump manufactured by Bartels Mikrotechnik.

The housing lid 850 may contain a display, such as an LCD display 860,that connects to the processor 600 and that can provide informationabout the system 800, such as, for example, diagnostic information,reaction parameters and/or finished product quality parameters, such as,for example, conductivity, redox, pH, UV spectrum and proteinconcentration.

The processor 600 in FIGS. 2, 3 and 4 may be implemented with a generalpurpose desktop computer or a general purpose laptop computer. Inaddition, the processor may be implemented with a tablet computer orsmartphone, such as iOS or Android-based tablets and smartphones.However, processor 600 can also be implemented with a special purposecomputer, programmed microprocessor or microcontroller and peripheralintegrated circuit elements, ASICs or other integrated circuits,hardwired electronic or logic circuits such as discrete elementcircuits, programmable logic devices such as FPGA, PLD, PLA or PAL orthe like. In general, any device on which a finite state machine capableof executing code for implementing the functionality described hereincan be used to implement the processor 600.

FIG. 5 shows a membrane chromatography component 310 that can be used insystems 700 and 800, in accordance with one preferred embodiment of thepresent invention. The membrane chromatography component 310 includes ahousing 2000 and porous membrane layers 2010 (preferably at least 10porous membrane layers). As discussed above, the individual porousmembrane layers 2010 preferably consist of an appropriate polymer, suchas polymethacrylate, that has been chemically functionalized with aligand, such as a diethylaminoethyl (DEAE), a quaternary amine (Q), or acarboxymethyl (CM) ligand for the case of ion-exchange chromatography,or a phenyl or butyl ligand for the case of hydrophobic interactionchromatography, or a mercaptoethylpyridine (MEP) ligand for the case ofmixed mode chromatography.

The membrane chromatography component 310 can be of any size, but in themicroscale embodiment of FIG. 4, it preferably has a volume capacity ofless than approximately 100 milliliters, and more preferably less thanapproximately 5 milliliters, in order to keep the system 800 relativelycompact. The membrane chromatography component 310 may be implemented,for example, with a Sartobind® Q SingelSep Nano manufactured bySartorius Stedim Biotech, which has a bed volume of 1 ml and a membranearea of 36 cm².

Raw product from reactor 210 is mixed with elution buffer solution viathree-way valve 2015, and the mixture enters the membrane chromatographycomponent 310 via inlet 2020. Purified product and waste exits via theoutlet 2030. Three-way valve 2040 directs the purified product to thediafiltration component 320/900/1100 and directs the waste to wastestorage 440.

FIGS. 6A-6C show a diafiltration component 900 that can be used insystems 700 and 800, in accordance with one preferred embodiment of thepresent invention. The diafiltration component 900 includesserpentine-shaped product and buffer sections 910 and 920, respectively.The diafiltration component 900 of FIGS. 6A-6C include a product section910 that is a serpentine-shaped channel formed on a first substrate1000. Similarly, the buffer section 920 is a channel formed on a secondsubstrate 1010 with the same serpentine shape as the product section910. A diafiltration membrane 930 is sandwiched between the first andsecond substrates 1000 and 1010, such that the serpentine-shapedchannels that form the product and buffer sections 910 and 910substantially overlap each other. The substrates 1000 and 1010 areattached to each other, with the diafiltration membrane 930 sandwichedbetween them, with any adhesive known in the art.

In the diafiltration component 900 of FIGS. 6A-6C, a diafiltrationbuffer solution flows through the serpentine-shaped product section 920and purified product from the membrane chromatography component 310flows through the serpentine-shaped product section 910. Diffusion takesplace from the product section 910 to the counterpart, similarly shapedbuffer section 920 via the diafiltration membrane 930.

The purified product from the membrane chromatography component 310enters the product section 910 via inlet buffer reservoir 1020 and inlet1030. The diafiltered product exits the product section 910 via outlet1040 and outlet buffer reservoir 1050. Diafiltration buffer enters thebuffer section 920 via inlet 1060 and exits the buffer section viaoutlet 1070. The diafiltration buffer is chosen to facilitate thetransfer of components through the diafiltration membrane 930, and couldbe, for example, 25 millimolar phosphoric acid titrated to pH 7 withsodium hydroxide, or 25 millimolar citric acid tritrated to pH 5 withsodium hydroxide.

The inlet and outlet buffer reservoirs 1020 and 1050 are optionally usedin order to dampen the back-and-forth oscillating flow, if needed. Amakeup buffer solution is preferably added to the diafiltered productvia the outlet buffer reservoir 1050 in order to replace the fluid thatwas that passed through the diafiltration membrane 930 with anequivalent volume of a different type of buffer, thereby transferringthe protein of interest to the makeup buffer. Alternatively, the volumeof the makeup buffer added via the outlet buffer reservoir 1050 can beless than the volume of fluid that has passed through the diafiltrationmembrane 930, in which case the diafiltration component 900 accomplishesboth buffer exchange and protein concentration.

As discussed above, diafiltration membrane 930 may suitably be ahydrophilic polymeric membrane, such as a polyethersulfone, acellulosic, or a polyvinylidene fluoride (PVDF) membrane with awell-defined pore structure that yields a desired molecular weightcut-off (MWCO) value in the range of 10 k to 200 kDa as appropriate fora given application.

FIG. 7 shows a diafiltration component 1100 in accordance with anotherembodiment of the present invention. The diafiltration component 1100may be used in system 700 or system 800 of FIGS. 3 and 4, respectively.The diafiltration component 1100 includes a buffer section 1120, and aproduct section 1110 that comprises tubing 1112 that is passed throughthe buffer section 1120. The tubing 1112 that makes up the productsection 1110 can be any type of tubing known in the art that canfunction as the dialysis membrane 1140 between the product 1115 in theproduct section 1110 and the buffer 1130 in the buffer section 1120.

The tubing 1112 is preferably flexible so that a larger amount of tubingcan be placed inside the solvent section 1120. The more tubing 1112 ispresent in the buffer section 1120, the more diffusion can take placebetween the tubing 1112 and the buffer 1130 due to the larger tubingsurface area in contact with the buffer 1130. End portions 1140 and 1150of the diafiltration component 1100 contain openings 1160 for the tubing1112 to enter and exit the diafiltration component 1100. The endportions 1140 and 1150 also contain an inlet 1170 for receivingdiafiltration buffer solution, and an outlet 1180 for expelling useddiafiltration buffer solution (waste). Although the diafiltrationcomponent 1100 is shown as rectangularly-shaped, it can be any othershape, such as cylindrically-shaped. Further, the diafiltrationcomponent 1100 can suitably be a flow cell that has been modified topass the tubing 1112 through the buffer section 1120.

Protein Expression in In Vivo and Cell-Free Systems

A protein is expressed in three main steps: replication, transcriptionand translation, as shown in FIG. 8. DNA multiplies to make multiplecopies by a process called replication. Transcription occurs when thedouble-stranded DNA is unwound to allow the binding of RNA polymeraseproducing messenger RNA (mRNA). Transcription is regulated at variouslevels by activators and repressors, and also by chromatin structure ineukaryotes. In prokaryotes, no special post-transcriptional modificationof mRNA is required. However, in eukaryotes, mRNA is further processedto remove introns (splicing), to add a ‘cap’ (M7 methyl-guanosine) atthe 5′ end and to add multiple adenosine ribonucleotides at the 3′ endof mRNA to generate a poly(A) tail. The modified mRNA is thentranslated.

The translation or protein synthesis is also a multi-step process withInitiation, Elongation and Termination steps and is similar in bothprokaryotes and eukaryotes. The difference is that in eukaryotes,proteins may undergo post-translational modifications, such asphosphorylation or glycosylation. The translation process requirescellular components such as ribosomes, transfer RNAs (tRNA), mRNA andprotein factors as well as small molecules like amino acids, ATP, GTPand other cofactors.

The difference between in vivo and in vitro (cell-free) proteinexpression is that in cell-free expression, the cell wall and the nucleiare no longer present.

Cell-Free Protein Expression from an Engineer's Perspective

To obtain the cell extract for cell-free protein expression, cells(E.coli, wheat germ, mammalian cells) are subjected to cell lysisfollowed by separation of the cell wall and nuclear DNA. The desiredprotein is synthesized by adding a DNA or mRNA template into the cellextract together with a reaction mix comprising of biological extractsand/or defined reagents. The reaction mix is comprised of amino acids,nucleotides, co-factors, enzymes and other reagents that are necessaryfor the synthesis, e.g. ribosomes, tRNA, polymerases, transcriptionalfactors, etc. When DNA is used as template (i.e. linked reaction), it isfirst transcribed to mRNA. Alternatively mRNA could also be useddirectly for translation.

The template for cell-free protein synthesis can be either mRNA or DNA.Translation of stabilized mRNA or combined transcription and translationconverts stored information into a desired protein. The combined system,generally utilized in E. coli systems, continuously generates mRNA froma DNA template with a recognizable promoter. Either endogenous RNApolymerase is used, or an exogenous phage RNA polymerase, typically T7or SP6, is added directly to the reaction mixture. Alternatively, mRNAcan be continually amplified by inserting the message into a templatefor QB replicase, an RNA dependent RNA polymerase. Purified mRNA isgenerally stabilized by chemical modification before it is added to thereaction mixture. Nucleases can be removed from extracts to helpstabilize mRNA levels. The template can encode for any particular geneof interest.

Salts, particularly those that are biologically relevant, such asmanganese, potassium or ammonium, may also be added. The pH of thereaction is generally run between pH 6-9. The temperature of thereaction is generally between 20° C. and 40° C. These ranges may beextended.

In addition to the above components such as cell-free extract, genetictemplate, and amino acids, other materials specifically required forprotein synthesis may be added to the reaction. These materials mayinclude salts, polymeric compounds, cyclic AMP, inhibitors for proteinor nucleic acid degrading enzymes, inhibitors or regulators of proteinsynthesis, oxidation/reduction adjusters, non-denaturing surfactants,buffer components, spermine, spermidine, etc.

The salts preferably include potassium, magnesium, ammonium andmanganese salts of acetic acid or sulfuric acid, and some of these mayhave amino acids as a counter anion. The polymeric compounds may bepolyethylene glycol, dextran, diethyl aminoethyl dextran, quaternaryaminoethyl and aminoethyl dextran, etc. The oxidation/reduction adjustermay be dithiothreitol (DTT), ascorbic acid, glutathione and/or theiroxides. Further DTT may be used as a stabilizer to stabilize enzymes andother proteins, especially if some enzymes and proteins possess freesulfhydryl groups. Also, a non-denaturing surfactant such as TritonX-100 may be used at a concentration of 0-0.5 M. Spermine and spermidinemay be used for improving protein synthetic ability, and cAMP may beused as a gene expression regulator.

Synthesized product is usually accumulated in the reactor within theproduction module, and then is isolated and purified according to themethods of the present invention for protein purification aftercompletion of the system operation. The amount of protein produced in atranslation reaction can be measured in various fashions. One methodrelies on the availability of an assay that measures the activity of theparticular protein being translated. Examples of assays for measuringprotein activity are a luciferase assay system and a chloramphenicolacetyl transferase assay system. These assays measure the amount offunctionally active protein produced from the translation reaction.Importantly, activity assays will not measure full length protein thatis inactive due to improper protein folding or lack of other posttranslational modifications necessary for protein activity. As usedherein, the term “activity” refers to a functional activity oractivities of a peptide or portion thereof associated with a full-length(complete) protein. Functional activities include, but are not limitedto, catalytic or enzymatic activity, antigenicity (ability to bind orcompete with a polypeptide for binding to an anti-polypeptide antibody),immunogenicity, ability to form multimers, and the ability tospecifically bind to a receptor or ligand for the polypeptide.Preferably, the activity of produced proteins retain at least 55%, 60%,65%, 70%, 80%, 85%, 90%, 95% or more of the initial activity for atleast 3 days at a temperature from about 0° C. to 30° C.

Another method of measuring the amount of protein produced in a combinedin vitro transcription and translation reactions is to perform thereactions using a known quantity of radiolabeled amino acid such as³⁵S-methionine or ¹⁴C-leucine and subsequently measuring the amount ofradiolabeled amino acid incorporated into the newly translated protein.Incorporation assays will measure the amount of radiolabeled amino acidsin all proteins produced in an in vitro translation reaction includingtruncated protein products.

In another study, expression of a fusion protein consisting of murineGM-C SF (granulocyte macrophage colony stimulating factor) and a scFvantibody, in reactor systems such as thin film, bubble column andEppendorf tube without membrane, were studied, producing protein upto >500 μg/ml protein with significant amount of precipitated protein(apprx eq.50%). Recently, rhGM-CF was expressed in a 100 L stirred tankreactor expressing protein up to 700 mg/L which was subsequentlypurified with DEAE resin, tangential flow filtration membrane (3 kD cutoff) and Sephacryl S-100 size exclusion chromatography with 99% purityand 65% recovery. Cell-free expression has not only been successful inthe expression of bacterial proteins, but also successfully producedglycoproteins like human choriogonadotropin (hCG) and envelopeglycoprotein (gp120) of human immunodeficiency virus type-1 (HIV-1) inhybridoma cell extract (HF10B4).

For protein purification, people have relied on column chromatographytraditionally, but in recent years membrane chromatography has emergedas an additional aid in this field, eliminating column chromatography atspecific steps like capture and polishing of protein at final step withoverall cost reduction up to 65%. Column chromatography is still usefulfor gradient purification of proteins, but membrane chromatography couldalso be studied by relying on the fact that step elution of protein andremoval of the impurities could be done at different buffer conditions.

The chart below compares cell-free and in vivo protein expressionsystems.

In vivo Cell free Biological cell required No cell, but cellularmachinery is required Time consuming process Time effective processToxic protein may be difficult to express Toxic protein could beexpressed Multiple steps in purification required Relatively less numberof steps required Higher fraction of misfolded protein along Reducedlevels of misfolded protein reported, with folded protein along withfolded protein but precipitated Higher endotoxins challenge Relativelyless endotoxins challenge Higher amount of impurities in crude proteinRelatively less impurities, enhancing capture causing challenges incapture step and increasing yield of the protein Established scale upHas significant potential to scale up Protein expression up to g/lProtein expression up to mg/l

Biomolecules for Protein Expression

The following biomolecules are preferably used for protein expression.To carry out a protein expression reaction, energy components and aminoacids are supplied externally and may include, but not limited to thefollowing components:

a. A genetic template for the target protein (mRNA or DNA) expression;b. T7 RNA polymerases for mRNA transcription;c. 9 Translation factors (initiation, elongation and termination);d. 20 aminoacyl-tRNA synthetases (ARSes) for esterification of aspecific amino acid to form an aminoacyl-tRNA;e. Methionyl-tRNA transformylase transfers hydroxymethyl-,formyl-groups;f. Creatine kinase converts ATP to ADP;g. Myokinase catalyzes the inter conversion of adenine nucleotides;h. Pyrophosphatase are acid anhydride hydrolases that act upondiphosphate bonds;i. 4 nucleoside triphosphates (ATP, GTP, CTP, TTP) for DNA formation;j. Creatine phosphate which serves as a reserve of high-energyphosphates for rapid mobilization;k. 10-formyl-5,6,7,8-tetrahydrofolate for the formylation of themethionyl initiator tRNA (fMet-tRNA);l. 20 amino acids for protein synthesis;m. Ribosomes for polypeptide translation;n. 46 tRNAs in protein synthesis; ando. Cellular components which assist in proper protein folding.

Some of the proteins that may be expressed by the present invention foron-demand production may include, but not limited to,adrenocorticotropic hormone peptides, adrenomedullin peptides,allatostatin peptides, amylin peptides, amyloid beta-protein fragmentpeptides, angiotensin peptides, antibiotic peptides, antigenicpolypeptides, anti-microbial peptides, apoptosis related peptides,atrial natriuretic peptides, bag cell peptides, bombesin peptides, boneGLA peptides, bradykinin peptides, brain natriuretic peptides,C-peptides, C-type natriuretic peptides, calcitonin peptides, calcitoningene related peptides, CART peptides, casomorphin peptides, chemotacticpeptides, cholecystokinin peptides, colony-stimulating factor peptides,corticortropin releasing factor peptides, cortistatin peptides, cytokinepeptides, dermorphin peptides, dynorphin peptides, endorphin peptides,endothelin peptides, ETa receptor antagonist peptides, ETh receptorantagonist peptides, enkephalin peptides, fibronectin peptides, galaninpeptides, gastrin peptides, glucagon peptides, Gn-RH associatedpeptides, growth factor peptides, growth hormone peptides, GTP-bindingprotein fragment peptides, guanylin peptides, inhibin peptides, insulinpeptides, interleukin peptides, laminin peptides, leptin peptides,leucokinin peptides, luteinizing hormone-releasing hormone peptides,mastoparan peptides, mast cell degranulating peptides, melanocytestimulating hormone peptides, morphiceptin peptides, motilin peptides,neuro-peptides, neuropeptide Y peptides, neurotropic factor peptides,orexin peptides, opioid peptides, oxytocin peptides, PACAP peptides,pancreastatin peptides, pancreatic polypeptides, parathyroid hormonepeptides, parathyroid hormone-related peptides, peptide T peptides,prolactin-releasing peptides, peptide YY peptides, renin substratepeptides, secretin peptides, somatostatin peptides, substance Ppeptides, tachykinin peptides, thyrotropin-releasing hormone peptides,toxin peptides, vasoactive intestinal peptides, vasopressin peptides,and virus related peptides.

Conventional and Non-Conventional Method of GBP Production

The systems and methods of the present invention can be used, forexample, for the cell-free expression and purification of glucosebinding protein (GBP). Glucose is a major carbon and energy source incellular metabolism of animal body and in bioprocess industry. Glucoseis not always beneficial in bioprocesses, it could also be detrimentalin bacterial culture leading to self-lysis of cells by formation ofacetate in Krebs cycle and reducing the pH of the culture. Thus, fastand efficient concentration detection of glucose is desired.

Glucose binding protein is a protein which could bind to glucose andserve this purpose by acting as a biosensor. A biosensor is ananalytical device used for the detection of an analyte that combines abiological component with a physicochemical detector component. GBP issuch a biosensor, where GBP binds with glucose and binding is analyzedusing fluorescence intensity and the corresponding signal is comparedwith standard glucose signal to estimate concentration of unknownsample. GBP is a monomeric periplasmic protein with molecular weight of34 kD (kilo Dalton) and is synthesized in the cytoplasm of E. coli.

In the conventional method, GBP (L225C mutant) is produced in multiplesteps, pre-inoculation of E. coli mutants in Luria Bertani (LB) broth,culturing, harvesting, cell washing, osmotic shock, labeling, liquidchromatography and dialysis. All these steps are time consuming (around4 days) and cumbersome. The present invention enables a non-conventionalcell free expression of GBP where expression is faster and the resultingprotein is relatively pure. This protein would preferably be labeledusing a fluorophore called acrylodan(6-Acryloyl-2-dimethylaminonaphthalene) and purified by D15 (DEAE)chromatography membrane. The protein would preferably further beconcentrated and dialyzed against 5 mM tris-HCl, pH 7.5.

Cell Free Method of Production of Granulocyte Colony Stimulating Factor(G-CSF) and pharmaceutical analog Fligrastim

For proof of principle, G-CSF also known as the pharmaceutical analogFilgrastim is used as a model therapeutic protein. Notably, the samemethod holds for any therapeutic protein for administration at thepoint-of-care. Filgrastim is used to stimulate the production ofgranulocytes (a type of white blood cell) in patients undergoing cancertherapy with specific drugs that are known to cause low white blood cellcounts.

Cell-free protein synthesis system was tested for G-CSF proteinexpression, the DNA used as the template in the system was G-CSFplasmid: 80 μg (concentration: 0.47 μg/μL) in combination withlyophilized CHO lysate in an amount of 1 mL, Gadd34-Myc plasmid 8 ug (@0.4 ug/uL)=20 uL)), Thermo Reaction Mix (5×): 400 uL, nuclease freewater: balance to 2 mL, and 1× CHO dialysis buffer at 25 mL. Six batcheswere run with a total batch volume for each batch of about 2 mL and theprocess took about 6 hours at a temperature of about 30° C. Thebioreactor used was SLIDE-A-LYZER™ dialysis cassette (10 kDa cutoff: 3mL).

About 1.98 mL of harvested product was subjected to purification in anIMAC spin column with loading buffer: 10 mM imidazole, wash buffer 1:10mM imidazole, wash buffer 2:30 mM imiadazole and elution buffer: 150 mMimidazole. Notably PBS buffer, without DTT, was used in the purificationprocess. The fractions were collected from triplicate runs where G-CSFwas expressed over a six hour period in the presently claimed cell-freesystem. The G-CSF was purified using a His-tagged affinity column. Thedata show the remarkable consistency of the expression and purificationof the target product.

FIGS. 9A and 9B show Western Blot results with an Anti-G-CSF antibody.The pellets discussed in both figures were washed once with 500 μL ofPBS and solubilized in 1500 μL of PBS with 1% Tween-20 and 1.5% TritonX-100. The “H” represents the Harvest, the “P” is the Pellet and the “E”is the Elute. The elution column shows a clear band representing G-CSFfor all three runs showing the remarkable consistency of the expressionand purification of the target product. The far right column shows theG-CSF standard that was also run. FIG. 9A shows the results of Run #3and FIG. 9B shows the results of Run #4. Clearly the results areconsistent and provide evidence that the process of the presentinvention is reproducible.

FIG. 10 A shows the quantified values of the harvested proteins andpurified protein of Run #3 of FIG. 9A and FIG. 10B show the values ofRun#4 of FIG. 9B.

Further it was shown that proteins produced in the on-demand system ofthe present invention provide for improved and increased potencyrelative to freeze/thaw data of the prior art method and it is evidentthat using a freeze/thaw cycle impacts activity. As shown in FIG. 11, inthe results of separate runs of 3 and 4, it can be seen that the freshlymade G-CSF has potency twice that of the reconstituted lyophilizedstandard. The same molecule loses its potency after just one freeze-thawcycle approaching that of a boiled control. These data prove ourassertion that administering a freshly made therapeutic protein (atmost, refrigerated for a few days) provides maximal potency and has theadditional advantage of no additives. This is a significant andsurprising improvement over the current paradigm of biologics productionand delivery.

In another example, the therapeutic protein Erythropoetin (EPO, used tostimulate red blood cell production in the human body) was produced inthe cell free system. FIG. 12 shows the same consistency of expressionin 4 separate batches as evidenced by the bands on the Western blot.

As the cell proliferation-based activity assay shows in the top panel ofFIG. 13A, the EPO in the extract is more active compared to controls. Itshould be noted that the EPO tested from the cell free process wasdiluted 100-fold, so the activity in the extract was in excess of100,000 units/mL. Given the typical EPO dosage is between 50-100units/mL/kg, it appears that 1 mL product contains sufficient EPO todose 10 adults. These data show the remarkable potential ofpoint-of-care manufacturing as the freshly expressed protein shows veryhigh activity. This is likely due to virtually no “aging” of the proteinthat normally takes place in conventionally manufactured proteins (i.e.deamidation, oxidation, aggregation etc.).

Streptokinase was also produced successfully in a cell free stirred tankbioreactor. A representative sample of activity at two harvest times isshown in FIG. 13B, lower panel. As can be seen, the harvest time may beused to pick a desired activity in the case of Streptokinase, severaldosing regimens are in use clinically and the harvest can be timed toconform to the desired dose, eliminating any dilution for the finaldelivery to obtain the correct dose. As can be seen, active EPO wasproduced and had extremely high activity (samples 32K14 and 36K14 werediluted 100 fold for the assay). For Streptokinase, lysate was harvestedat two time points and activity measured. This approach may be used todetermine the dose needed for delivery to the patient.

That which is claimed is:
 1. A method of stimulating production ofgranulocytes in a patient undergoing cancer therapy, said methodcomprising administering a Granulocyte Colony Stimulating Factor (G-CSF)protein to the patient, wherein the G-CSF is synthesized on-demand in abioprocessing system using cell-free protein expression, saidbioprocessing system comprising: a production module for producingnon-purified G-CSF protein, and a purification module for receiving thenon-purified G-CSF protein from the production module and for purifyingthe G-CSF protein from reagents.
 2. The method of claim 1, wherein theG-CSF protein can be administered continuously or as a bolus to thepatient.
 3. The method of claim 1, wherein the purification modulecomprises: a chromatography component for receiving the non-purifiedG-CSF protein from the production module and for outputting purifiedG-CSF protein; and a diafiltration component for receiving the purifiedG-CSF protein from the chromatography component and for outputtingfurther purified G-CSF protein, wherein the diafiltration componentcomprises a product section for receiving the purified G-CSF proteinfrom the chromatography component and a buffer section for receiving abuffer solution.
 4. The method of claim 3, wherein the buffer solutionis free of dithiothreitol (DTT).
 5. The method of claim 1, wherein theproduction module comprises a reaction mixture comprising a nucleotidetemplate for production of the G-CSF protein; monomers for the G-CSFprotein to be synthesized, co-factors, enzymes and reagents that arenecessary for the synthesis.
 6. The method of claim 5, wherein theenzymes and reagents that are necessary for the synthesis are ribosomes,tRNA, polymerases and transcriptional factors.
 7. The method of claim 1,wherein the production module comprises a bioreactor for cell-free G-CSFprotein expression.
 8. The method of claim 1, wherein the diafiltrationcomponent further comprises: a first substrate; a second substrate; anda diafiltration membrane positioned between the first and secondsubstrates.
 9. The method of claim 8, wherein the diafiltrationcomponent comprises a flow cell.
 10. The method of claim 1, wherein theproduction module comprises at least one sensor for monitoring at leastone of conductivity, temperature, pH, oxygen and CO₂.
 11. The method ofclaim 1, wherein the production module and purification module eachcomprise a heating and cooling element for controlling the temperatureof solution inside the production module and purification module. 12.The method of claim 1, further comprising a fluid storage and dispensingmodule for storing solutions used by the production module for G-CSFprotein expression, for storing waste product produced by thepurification module, and for storing G-CSF protein output by thepurification module.
 13. The method of claim 1, wherein thebioprocessing system further comprises a processor for controllingand/or monitoring at least one of the production module and thepurification module.
 14. The method of claim 1, wherein a therapeuticdose and potency/activity of the G-CSF protein is determined byexpression time in the production module.
 15. The method of claim 1,wherein the G-CSF protein is delivered directly to the patient.
 16. Themethod of claim 1, wherein a therapeutic dose and potency/activity ofthe G-CSF protein is determined by holding time in the productionmodule.
 17. The method of claim 1, wherein potency/activity of thepurified G-CSF protein is at least 55% or more of the initial activityfor at least 3 days at temperature from above 0° C. to about 30° C. 18.The method of claim 1, wherein the cancer therapy comprises drugs thatcause low white blood cell counts in the patient.
 19. A method oftreating anemia in a patient in need thereof, said method comprisingadministering Erythropoetin (EPO) to the patient, wherein the EPO issynthesized on-demand in a bioprocessing system using cell-free proteinexpression, said bioprocessing system comprising: a production modulefor producing non-purified EPO protein, and a purification module forreceiving the non-purified EPO protein from the production module andfor purifying the EPO protein from reagents.
 20. A method of treating aclot or achieving thrombolysis in a patient in need thereof, said methodcomprising administering Streptokinase to the patient, wherein theStreptokinase is synthesized on-demand in a bioprocessing system usingcell-free protein expression, said bioprocessing system comprising: aproduction module for producing non-purified Streptokinase protein, anda purification module for receiving the non-purified Streptokinaseprotein from the production module and for purifying the Streptokinaseprotein from reagents.